Process for removal of carbon dioxide from a gas

ABSTRACT

The invention provides a process for the removal of CO 2  from a gas, the process comprising the steps of: (a) removing CO 2  from the gas by contacting the gas with absorbing liquid in an absorber to obtain absorbing liquid enriched in CO 2  and a purified gas; (b) heating absorbing liquid enriched in CO 2  (c) contacting heated absorbing liquid enriched in CO 2  with a stripping gas at elevated temperature in a regenerator to obtain regenerated absorbing liquid and a hot gas stream enriched in CO 2  wherein at least part of the absorbing liquid enriched in CO 2  is heated through external heat exchange with the hot gas stream enriched in CO 2 .

The present application claims priority from European Patent Application 08102564.5 filed 13 Mar. 2008.

The invention relates to a process for removal of carbon dioxide (CO₂) from a gas.

During the last decades there has been a substantial global increase in the amount of CO₂ emission to the atmosphere. Emissions of CO₂ into the atmosphere are thought to be harmful due to its “greenhouse gas” property, contributing to global warming. Following the Kyoto agreement, CO₂ emission has to be reduced in order to prevent or counteract unwanted changes in climate. The largest sources of CO₂ emission are combustion of fossile fuels, for example coal or natural gas, for electricity generation and the use of petroleum products as a transportation and heating fuel. These processes result in the production of gases comprising CO₂. Thus, removal of at least part of the CO₂ prior to emission of these gases into the atmosphere is desirable.

Processes for removal of CO₂ from gases are known in the art. For example, in EP 0,744,987 a process for removing and preventing emissions of CO₂ into the atmosphere is described. In the process described in EP 0,744,987, CO₂ is transferred from exhaust gas exiting a gas turbine to an absorption liquid, followed by regeneration at elevated temperatures to release absorbed CO₂ from the absorbing liquid. A severe drawback of the process described in EP 0,744,987 is the high energy consumption, leading to a lower overall energy output. To improve the efficiency, the exhaust gas exiting the gas turbine is passed through a heat recovery steam generator, producing high pressure steam and low pressure steam. The low pressure steam is used to achieve the elevated temperatures needed for the regeneration of the absorbing liquid. Although this results in a better overall efficiency, additional equipment is needed.

Thus, there remains a need for a simple, energy-efficient process for removal of CO₂ from gases.

To this end, the invention provides a process for the removal of CO₂ from a gas, the process comprising the steps of:

(a) removing CO₂ from the gas by contacting the gas with absorbing liquid in an absorber to obtain absorbing liquid enriched in CO₂ and a purified gas;

(b) heating absorbing liquid enriched in CO₂;

(c) contacting heated absorbing liquid enriched in CO₂ with a stripping gas at elevated temperature in a regenerator to obtain regenerated absorbing liquid and a hot gas stream enriched in CO₂; wherein at least part of the absorbing liquid enriched in CO₂ is heated through external heat exchange with the hot gas stream enriched in CO₂.

External heat exchange as used herein refers to the event that the hot gas stream enriched in CO₂ is led from the regenerator to at least one heat exchanger, wherein heat is recovered from the hot gas stream enriched in CO₂ and the heat recovered is used in the regeneration step.

The process enables simple and more energy-efficient removal of CO₂ using an absorbing liquid, because part of the heat requirement for warming the absorbing liquid enriched in CO₂ is provided by the hot gas stream enriched in CO₂. It is believed that the heat requirement is delivered by at least partly condsing the steam that is present in the hot gas stream enriched in CO₂. Suitably, the process leads to an improvement in the overall energy efficiency by 5 to 25%, preferably by 10 to 25%.

An embodiment of the present invention will now be described by way of example only, and with reference to the accompanying non-limiting drawing in which:

FIG. 1 is a scheme of a process for the removal of CO₂ from a gas according to one embodiment of the invention. For the purpose of this description, a single reference number will be assigned to a line as well as stream carried in that line.

In step (a), CO₂ is removed by contacting the gas with an absorbing liquid at elevated pressure, suitably in an absorber. In the figure, the gas is led via line 1 to absorber 2. Suitably, in the event that the gas is a flue gas, absorption takes place at relatively low temperature and relatively low pressure. Suitably, the gas is cooled prior to entering the absorber.

The process is suitable for any gas comprising CO₂. For example, the gases to be treated may be natural gas, synthesis gas, obtained for instance by (catalytic) partial oxidation and/or by steam methane reforming of hydrocarbons, e.g. methane, natural or associated gas, naphtha, diesel and liquid residual fractions, gases originating from coal gasification, coke oven gases, refinery gases, hydrogen and hydrogen containing gases, and flue gases.

Suitably, the gas comprises in the range of from 0.25 to 70% (v/v) of CO₂, preferably from 1 to 45% (v/v).

In the event that the gas is a flue gas, the amount of CO₂ will generally be lower, suitably from 0.25 to 20% (v/v) and the gas will usually also comprise oxygen, preferably in the range of from 0.25 to 20% (v/v), more preferably from 0.5 to 15% (v/v), still more preferably from 1 to 10% (v/v).

The absorbing liquid may be any absorbing liquid capable of removing CO₂ from a gas stream. Such absorbing liquids may include chemical solvents or combinations of chemical and physical solvents.

Suitable chemical solvents include ammonia and amine compounds.

One preferred absorbing liquid comprises one or more amines. It has been found that amines are especially suitable for removal of CO2 from gases.

The amines may be single primary or secondary or tertiary amines, preferably derived from ethanol amine, or may be mixtures of primary or secondary amines and/or tertiary amines.

Preferably, the one or more amines are selected from the group of monethanolamine (MEA), diethanolamine (DEA), diglycolamine (DGA), methyldiethanolamine (MDEA), triethanolamine (TEA), N,N′-di(hydroxyalkyl)piperazine, N,N,N′,N′-tetrakis(hydroxyalkyl)-1,6-hexanediamine and tertiary alkylamine sulfonic acid compounds.

MEA is an especially preferred amine, due to its ability to absorb a relatively high percentage of CO₂ (volume CO₂ per volume MEA). Thus, an absorbing liquid comprising MEA is suitable to remove CO₂ from gases having low concentrations of CO₂, typically 3 to 10% (v/v) of CO₂.

Preferably, the N,N′-di(hydroxyalkyl)piperazine is N,N′-d-(2-hydroxyethyl)piperazine and/or N,N′-di-(3-hydroxypropyl)piperazine.

Preferably, the tetrakis(hydroxyalkyl)-1,6-hexanediamine is N,N,N′,N′-tetrakis(2-hydroxyethyl)-1,6-hexanediamine and/or N,N,N′,N′-tetrakis(2-hydroxypropyl)-1,6-hexanediamine.

Preferably, the tertiary alkylamine sulfonic compounds are selected from the group of 4-(2-hydroxyethyl)-1-piperazineethanesulfonic acid, 4-(2-hydroxyethyl)-1-piperazinepropanesulfonic acid, 4-(2-hydroxyethyl)piperazine-1-(2-hydroxypropanesulfonic acid) and 1,4-piperazinedi(sulfonic acid).

As especially preferred absorbing liquid comprises mixtures of a primary or secondary amine with a tertiary or a sterically hindered amine. Suitable tertiary or sterically hindered amines have been described hereinabove. The primary or secondary amine compound suitably has a pKb (at 25° C. in water) below 5.5, preferably below 5, more preferably below 4.5. A lower pKb results in improved process results in the form of increased CO₂ absorption. An especially preferred secondary amine is piperazine.

In the event that the gas stream comprises an appreciable quantity of oxygen, suitably in the range of from 1 to 20% (v/v) of oxygen, preferably a corrosion inhibitor is added to the absorbing liquid. Suitable corrosion inhibitors are described for example in U.S. Pat. No. 6,036,888.

It will be understood that the conditions used for absorption (step a) depend inter alia on the type of absorbing liquid used.

In the event that the absorbing liquid comprises an amine, step (a) is suitably carried out at a temperature between 15 and 90° C., preferably at a temperature of at least 20° C., more preferably between 25 and 80° C., still more preferably between 40 and 65° C., and even still mote preferably at about 55° C.

In the event that the absorbing liquid comprises ammonia, suitably the absorbing step is performed at temperatures below ambient temperature, preferably in the range of from 0 to 10° C., more preferably from 2 to 8° C.

In the event that the absorbing liquid comprises an amine, step (a) is suitably carried out at a pressure between 10 and 150 bar, especially between 25 and 90 bara.

Step (a) results in purified gas and absorbing liquid rich in CO₂. Suitably, more than 80%, preferably more than 90% and more preferably more than 95% of the CO₂ is removed. As the purified gas comprises low concentrations of CO₂, it may now be vented into the atmosphere, or used elsewhere.

In step (b), the absorbing liquid rich in CO₂ is heated, suitably using the regenerated absorbing liquid of step (c). This heating step effects that the absorbing liquid rich in CO₂ is brought to a temperature close to or in the range of the temperature at which regeneration of absorbing liquid rich in CO₂ will take place. Suitably, step (b) is performed via heat exchange of the absorbing liquid rich in CO₂ with a hot gas or liquid. As will be explained hereinafter, at least part of the heat requirements of step (b) are fulfilled using heat from a hot stripping gas comprising CO₂ generated in the regeneration step.

In step (c), the heated absorbing liquid rich in CO₂ (transferred via line 8 in the figure) is contacted with a stripping gas at elevated temperature in a regenerator (9 in the figure) to obtain regenerated absorbing liquid and a gas stream enriched in carbon dioxide. In the figure, the gas stream enriched in CO₂ is led from the regenerator via line 10 to a heat exchanger 11.

It will be understood that the conditions used for regeneration depend inter alia on the type of absorbing liquid and on the conditions used in the absorption step. Suitably, regeneration takes place at a different temperature and/or different pressure than the absorption. The regeneration step is suitably performed at temperatures higher than used in the absorption step.

In the event that the absorbing liquid comprises an amine, preferred regeneration temperatures are in the range of from 100 to 200° C. In the event that the absorbing liquid comprises an aqueous amine, regeneration preferably takes place at pressure in the range of from 1 to 5 bara.

When using an absorbing liquid comprising ammonia, the CO₂-enriched gas stream exiting the regenerator has an elevated pressure. Suitably, the pressure of the CO₂-enriched gas stream is in the range of from 5 to 30 bara, preferably from 8 to 30 bara. In applications where the CO₂-enriched gas stream needs to be at a high pressure, for example when it will be used for injection into a subterranean formation, it is an advantage that the CO₂-enriched gas stream is already at an elevated pressure. In a preferred embodiment, the pressurised CO₂-enriched gas stream is used for enhanced oil recovery, suitably by injecting it into an oil reservoir where it tends to dissolve into the oil in place, thereby reducing its viscosity and thus making it more mobile for movement towards the producing well. Normally, a series of compressors is needed to pressurise the CO₂-enriched gas stream to the desired high pressures. A CO₂-enriched gas stream which is already at elevated pressure is easier to further pressurise.

In the process, at least part of the absorbing liquid enriched in CO₂ is heated through heat exchange with the hot gas stream enriched in CO₂. This can be achieved in several ways. A preferred embodiment will be described in detail. It will however be understood that the invention is not limited to this preferred embodiment; many variations are possible and these are also comprised in the invention.

In the preferred embodiment, the absorbing liquid enriched in CO₂ is split into two fractions, as shown in the figure, wherein two streams are led via lines 6 and 12 from splitter 5. A first fraction of the absorbing liquid enriched in CO₂ is led to a first heat exchanger, 7 in the figure, thereby heating said first part of the absorbing liquid enriched in CO₂ using a regenerated absorption liquid. A second fraction of the absorbing liquid enriched in CO₂ is led to a second heat exchanger, 11 in the figure, thereby heating said second part of the absorbing liquid enriched in CO₂. The hot gas stream enriched in CO₂ is led to the second heat exchanger and used to heat the second part of the absorbing liquid enriched in CO₂ through heat exchange. Preferably, the first fraction is larger than the second fraction. The ratio between the first and the second fraction will depend inter alia on the absorbing liquid used, as different absorbing liquids will have different heat requirements. A preferred ratio between the first and second fraction of the absorbing liquid enriched in CO₂ is in the range of from 1:1 to 9:1, more preferably from 1:1 to 4:1, still more preferably about 7:3.

In the figure, gas comprising CO₂ is led via line 1 to absorber 2. In absorber 2, the gas is contacted with absorbing liquid, thereby transferring CO₂ from the gas to the absorbing liquid to obtain purified gas and absorbing liquid enriched in CO₂. The purified gas is led from the absorber via line 3. The absorbing liquid enriched in CO₂ is led from the absorber via line 4 to a splitter 5, where it is split into two streams.

A first stream is led via line 6 to a first heat exchanger 7, where it is heated. Resulting heated absorbing liquid enriched in CO₂ is led via line 8 to regenerator 9. In regenerator 9, heated absorbing liquid enriched in CO₂ is contacted as elevated temperature with a stripping gas, thereby transferring CO₂ from the absorbing liquid to the stripping gas to obtain regenerated absorbing liquid and hot stripping gas enriched in CO₂. The hot stripping gas enriched in CO₂ is led from the regenerator via line 10 to heat exchanger 11.

A second stream of absorbing liquid enriched in CO₂ is led from splitter 5 via line 12 to heat exchanger 11. In heat exchanger 11, the absorbing liquid enriched in CO₂ is heated against the hot stripping gas enriched in CO₂. The resulting heated absorbing liquid enriched in CO₂ is lead from heat exchanger 11 via line 13 to regenerator 9.

Cooled stripping gas enriched in CO₂ is led from heat exchanger 11 via line 14 to condenser 15, where water is condensed. The cooled stream is led via line 16 to separator 17, where condensed water is separated and led via line 18 to regenerator 9. The gas stream enriched in CO₂, depleted of water is led via line 19 to compressor 20, where it is pressurised. The pressurised CO₂ stream is led from the compressor via line 21 to be used elsewhere.

Regenerated absorbing liquid is withdrawn from the bottom of regenerator 9 via line 22 and led to a reboiler 23, where it is heated producing stripping steam and a regenerated absorption liquid. The stripping steam is led via line 24 to the regenerator. The hot regenerated absorbing liquid is led via line 25 to heat exchanger 7, where it is cooled against absorbing liquid comprising CO₂. Cooled regenerated absorbing liquid is led via line 26 to absorber 2.

The invention is illustrated using the following non-limiting examples.

EXAMPLE 1 According to the Invention

In a process as described in the Figure, a flue gas comprising 4.1% CO₂ is routed via line 1 to absorber column 2 with a flow rate of 499.1 Nm3/s. In the absorber, 85% of the CO₂ is absorbed. 18% of the CO₂-enriched solvent stream leaving the absorber 2 via line 4 is led via heat exchanger 11 to column 9. The remainder of the stream leaving absorber 2 via line 4 is led to heat exchanger 7. This results in a duty of reboiler 23 of 231.1 MW.

EXAMPLE 2 According to the Invention

The process as described above was repeated but now all solvent leaving the absorber 2 via line 4 is routed via heat exchanger 7 to regenerator 9. This results in duty of reboiler 23 of 253.3 MW.

Hence, the process enables a reduction in reboiler duty of about 9%. 

What is claimed is:
 1. A process for removing CO₂ from a gas, the process comprising the steps of: (a) removing CO₂ from the gas by contacting the gas with an absorbing liquid selected from either N,N′-di(hydroxyalkyl)piperazine, N,N,N′,N′-tetrakis(hydroxyalkyl)-1,6-hexanediamine or tertiary alkylamine sulfonic acid compounds in an absorber to obtain an absorbing liquid enriched in CO₂ and a purified gas; (b) heating the absorbing liquid enriched CO₂ to obtain a heated absorbing liquid enriched in CO₂; and (c) contacting the heated absorbing liquid enriched in CO₂ with a stripping gas at an elevated temperature in a regenerator to obtain a regenerated absorbing liquid and a hot gas stream enriched in CO₂; wherein 30% of the absorbing liquid enriched in CO₂ is heated through external heat exchange with the hot gas stream enriched in CO₂.
 2. A process according to claim 1, wherein the absorbing liquid enriched in CO₂ is split into a first part of absorbing liquid enriched in CO₂ and a second part of absorbing liquid enriched in CO₂; the first part of absorbing liquid enriched in CO₂ is led to a first heat exchanger, thereby heating the first part of absorbing liquid enriched in CO₂; the second part of absorbing liquid enriched in CO₂ is led to a second heat exchanger, thereby heating said second part of absorbing liquid enriched in CO₂; and the hot gas stream enriched in CO₂ is led to the second heat exchanger and used to heat the second part of absorbing liquid enriched in CO₂ through heat exchange.
 3. A process according to claim 1, wherein the absorbing liquid further comprises a physical solvent.
 4. A process according to claim 1, wherein the absorbing liquid comprises ammonia.
 5. A process according to claim 1, wherein the pressure of the CO₂-enriched gas stream is in the range of from 5 to 30 bara.
 6. A process according to claim 1, wherein the gas stream enriched in CO₂ is pressurised using a carbon dioxide compressor to produce a pressurised carbon dioxide stream.
 7. A process according to claim 6, wherein the pressurised carbon dioxide stream is yielded to a process for enhanced oil recovery.
 8. A process for removing CO₂ from a gas comprising CO₂, the process comprising: removing CO₂ from the gas by contacting the gas with an absorbing liquid, wherein the absorbing liquid comprises a compound selected from the group consisting of a N,N′-di(hydroxyalkyl)piperazine, a N,N,N′,N′-tetrakis(hydroxyalkyl)-1,6-hexanediamine, and a tertiary alkylamine sulfonic acid compound, to obtain a CO₂-enriched absorbing liquid enriched and a purified gas heating the CO₂-enriched absorbing; stripping CO₂ from the CO₂-enriched absorbing liquid through contact with a striping gas at an elevated temperature to obtain a regenerated absorbing liquid and a CO₂-enriched stripping gas; and, heating 30% of the CO₂-enriched absorbing liquid through heat exchange with the CO₂-enriched stripping gas.
 9. The process of claim 8, wherein the N,N′-di(hydroxyalkyl)piperazine is either N,N′-di-(2-hydroxyethyl)piperazine or N,N′-di-(3-hydroxypropyl)piperazine.
 10. The process of claim 8, wherein the N—N—N′—N′-tetrakis(hydroxyalkyl)-1,6-hexanediamine is either N,N,N′N′-tetrakis(2-hydroxyethyl)-1,6-hexanediamine or N,N,N′,N′-tetrakis(2-hydroxypropyl)-1-6-hexanediamine.
 11. The process of claim 8, wherein the tertiary alkylamine sulfonic acid is selected from the group consisting of 4-(2-hydroxyethyl)-1-piperazineethanesulfonic acid, 4-(2-hydroxyethyl)-1-piperazinepropanesulfonic acid, 4-(2-hydroxyethyl)piperazine-1-(2-hydroxypropanesulfonic acid) and 1,4-piperazinedi(sulfonic acid).
 12. The process of claim 8, wherein the gas further comprises oxygen and the absorbing liquid further comprises a corrosion inhibitor.
 13. The process of claim 8, wherein the contacting of the gas with the absorbing liquid is performed at a temperature between 15° C. and 90° C.
 14. The process of claim 8, wherein the CO₂-enriched stripping gas has a pressure between 10 bar and 150 bar. 